Evaporative fuel vapor emission control systems

ABSTRACT

An evaporative emission control canister system comprises an initial adsorbent volume having an effective incremental adsorption capacity at 25° C. of greater than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane, and at least one subsequent adsorbent volume having an effective incremental adsorption capacity at 25° C. of less than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane, an effective butane working capacity (BWC) of less than 3 g/dL, and a g-total BWC of between 2 grams and 6 grams. The evaporative emission control canister system has a two-day diurnal breathing loss (DBL) emissions of no more than 20 mg at no more than 210 liters of purge applied after the 40 g/hr butane loading step.

TECHNICAL FIELD

The present disclosure, in various embodiments, relates generally to evaporative emission control systems. More particularly, the present disclosure relates to evaporative fuel vapor emission control systems.

BACKGROUND

Evaporation of gasoline fuel from motor vehicle fuel systems is a major potential source of hydrocarbon air pollution. Such emissions can be controlled by the canister systems that employ activated carbon to adsorb the fuel vapor emitted from the fuel systems. Under certain modes of engine operation, the adsorbed fuel vapor is periodically removed from the activated carbon by purging the canister systems with ambient air to desorb the fuel vapor from the activated carbon. The regenerated carbon is then ready to adsorb additional fuel vapor.

An increase in environmental concerns has continued to drive strict regulations of the hydrocarbon emissions from motor vehicles even when the vehicles are not operating. When a vehicle is parked in a warm environment during the daytime heating (i.e., diurnal heating), the temperature in the fuel tank increases resulting in an increased vapor pressure in the fuel tank. Normally, to prevent the leaking of the fuel vapor from the vehicle into the atmosphere, the fuel tank is vented through a conduit to a canister containing suitable fuel adsorbent materials that can temporarily adsorb the fuel vapor. The fuel vapor from the fuel tank enters the canister through a fuel vapor inlet of the canister and diffuses into the adsorbent volume where it is adsorbed in temporary storage before being released to the atmosphere through a vent port of the canister. Once the engine is turned on, ambient air is drawn into the canister system through the vent port of the canister. The purge air flows through the adsorbent volume inside the canister and desorbs the fuel vapor adsorbed on the adsorbent volume before entering the internal combustion engine through a fuel vapor purge conduit. The purge air does not desorb the entire fuel vapor adsorbed on the adsorbent volume, resulting in a residue hydrocarbon (“heel”) that may be emitted to the atmosphere. In addition, that heel in local equilibrium with the gas phase also permits fuel vapors from the fuel tank to migrate through the canister system as emissions. Such emissions typically occur when a vehicle has been parked and subjected to diurnal temperature changes over a period of several days, commonly called “diurnal breathing losses.” The California Low Emission Vehicle Regulation makes it desirable for these diurnal breathing loss (DBL) emissions from the canister system to be below 10 mg (“PZEV”) for a number of vehicles beginning with the 2003 model year and below 50 mg, typically below 20 mg, (“LEV-II”) for a larger number of vehicles beginning with the 2004 model year. Now the California Low Emission Vehicle Regulation (LEV-III) requires canister DBL emissions not to exceed 20 mg as per the Bleed Emissions Test Procedure (BETP) as written in the California Evaporative Emissions Standards and Test Procedures for 2001 and Subsequent Model Motor Vehicles, Mar. 22, 2012.

Several approaches have been reported to reduce the diurnal breathing loss (DBL) emissions. One approach is to significantly increase the volume of purge gas to enhance desorption of the residue hydrocarbon heel from the adsorbent volume. This approach, however, has the drawback of complicating management of the fuel/air mixture to the engine during purge step and tends to adversely affect tailpipe emissions. See U.S. Pat. No. 4,894,072.

Another approach is to design the canister to have a relatively low cross-sectional area on the vent-side of the canister, either by the redesign of existing canister dimensions or by the installation of a supplemental vent-side canister of appropriate dimensions. This approach reduces the residual hydrocarbon heel by increasing the intensity of purge air. One drawback of such approach is that the relatively low cross-sectional area imparts an excessive flow restriction to the canister. See U.S. Pat. No. 5,957,114.

Another approach for increasing the purge efficiency is to heat the purge air, or a portion of the adsorbent volume having adsorbed fuel vapor, or both. However, this approach increases the complexity of control system management and poses some safety concerns. See U.S. Pat. Nos. 6,098,601 and 6,279,548.

Another approach is to route the fuel vapor through an initial adsorbent volume and then at least one subsequent adsorbent volume prior to venting to the atmosphere, wherein the initial adsorbent volume has a higher adsorption capacity than the subsequent adsorbent volume. See U.S. Pat. No. RE38,844.

The regulations on diurnal breathing loss (DBL) emissions continue to drive new developments for improved evaporative emission control systems, especially when the level of purge air is low. Furthermore, the diurnal breathing loss (DBL) emissions may be more severe for a hybrid vehicle that includes both an internal combustion engine and an electric motor. In such hybrid vehicles, the internal combustion engine is turned off nearly half of the time during vehicle operation. Since the adsorbed fuel vapor on the adsorbents is purged only when the internal combustion engine is on, the adsorbents in the canister of a hybrid vehicle is purged with fresh air less than half of the time compared to conventional vehicles. A hybrid vehicle generates nearly the same amount of evaporative fuel vapor as the conventional vehicles. The lower purge frequency of the hybrid vehicle can be insufficient to clean the residue hydrocarbon heel from the adsorbents in the canister, resulting in high diurnal breathing loss (DBL) emissions.

Accordingly, it is desirable to have an evaporative emission control system with low diurnal breathing loss (DBL) emissions even when a low level of purge air is used, or when the adsorbents in the canister are purged less frequently such as in the case of hybrid vehicles, or both. Though a passive approach has been greatly desired, existing passive approaches still leave DBL emissions at levels that are many times greater than the 20 mg LEV-III requirement when only a fraction of the historically available purge is now available.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a cross-sectional view of the evaporative emission control canister system according to one embodiment of the disclosure, wherein the canister system has one canister;

FIG. 2 is a cross-sectional view of the evaporative emission control canister system according to one embodiment of the disclosure, wherein the canister system has one canister;

FIG. 3 is a cross-sectional view of the evaporative emission control canister system according to one embodiment of the disclosure, wherein the canister system has one canister;

FIG. 4 is a cross-sectional view of the evaporative emission control canister system according to one embodiment of the disclosure, wherein the canister system has a main canister and a supplemental canister;

FIG. 5 is a cross-sectional view of the evaporative emission control canister system according to one embodiment of the disclosure, wherein the canister system has a main canister and a supplemental canister;

FIG. 6 is a cross-sectional view of the evaporative emission control canister system according to one embodiment of the disclosure, wherein the canister system has a main canister and a supplemental canister;

FIG. 7 is a cross-sectional view of the evaporative emission control canister system according to one embodiment of the disclosure, wherein the canister system has a main canister and a supplemental canister;

FIG. 8 is a simplified schematic drawing of the apparatus used for the determination of the butane adsorption capacity; and

FIGS. 9-22 are simplified schematic drawings of the evaporative emission control canister systems according to some non-limiting embodiments of present disclosure.

DESCRIPTION

The present disclosure now will be described more fully hereinafter, but not all embodiments of the disclosure are shown. While the disclosure has been described with reference to exemplary embodiments, it will be understood by those skilled in the art that various changes may be made and equivalents may be substituted for elements thereof without departing from the scope of the disclosure. In addition, many modifications may be made to adapt a particular structure or material to the teachings of the disclosure without departing from the essential scope thereof.

The drawings accompanying the application are for illustrative purposes only. They are not intended to limit the embodiments of the present application. Additionally, the drawings are not drawn to scale. Elements common between figures may retain the same numerical designation.

In a particular embodiment, an evaporative emission control canister system includes one or more canisters. The evaporative emission control canister system comprises an initial adsorbent volume having an effective incremental adsorption capacity at 25° C. of greater than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane; and at least one subsequent adsorbent volume having an effective incremental adsorption capacity at 25° C. of less than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane, an effective butane working capacity (BWC) of less than 3 g/dL, and a g-total BWC of between 2 grams and 6 grams. The initial adsorbent volume and the at least one subsequent adsorbent volume are located within a single canister, or the initial adsorbent volume and the at least one subsequent adsorbent volume are located in separate canisters that are connected to permit sequential contact by fuel vapor. The evaporative emission control canister system has a two-day diurnal breathing loss (DBL) emissions of no more than 20 mg at no more than about 210 liters of purge applied after the 40 g/hr butane loading step.

FIG. 13 show non-limiting examples of some embodiments of the evaporative emission control canister system wherein an initial adsorbent volume and subsequent adsorbent volume(s) are located within a single canister. FIGS. 4-7 show non-limiting examples of the embodiments of the evaporative emission control canister system that includes more than one canister, wherein an initial adsorbent volume and at least one subsequent adsorbent volume are located in separate canisters that are connected to permit sequential contact by fuel vapor.

FIG. 1 illustrates one embodiment of the evaporative emission control canister system having an initial adsorbent volume and a subsequent adsorbent volume within a single canister. Canister system 100 includes a support screen 102, a dividing wall 103, a fuel vapor inlet 104 from a fuel tank, a vent port 105 opening to an atmosphere, a purge outlet 106 to an engine, an initial adsorbent volume 201, and a subsequent adsorbent volume 202.

When an engine is off, the fuel vapor from a fuel tank enters the canister system 100 through the fuel vapor inlet 104. The fuel vapor diffuses into the initial adsorbent volume 201, and then the subsequent adsorbent volume 202 before being released to the atmosphere through the vent port 105 of the canister system. Once the engine is turned on, ambient air is drawn into the canister system 100 through the vent port 105. The purge air flows through the subsequent adsorbent volume 202 and then the initial adsorbent volume 201, and desorbs the fuel vapor adsorbed on the adsorbent volumes 202, 201 before entering an internal combustion engine through the purge outlet 106.

The evaporative emission control canister system may include more than one subsequent adsorbent volume. By way of non-limiting example, the evaporative emission control canister system 100 may include an initial adsorbent volume 201 and three subsequent adsorbent volumes 202, 203, 204 within a single canister, as illustrated in FIG. 2.

Additionally, the evaporative emission control canister system may include an empty volume within the canister. As used herein, the term “empty volume” refers to a volume not including any adsorbent. Such volume may comprise any non-adsorbent including, but not limited to, air gap, foam spacer, screen, or combinations thereof. In a non-limiting example shown in FIG. 3, the evaporative emission control canister system 100 may include an initial adsorbent volume 201; three subsequent adsorbent volumes 202, 203, 204 within a single canister; and an empty volume 205 between the subsequent adsorbent volumes 203 and 204.

By way of non-limiting example, FIGS. 4-7 shows the embodiments of the evaporative emission control canister system wherein the canister system includes more than one canister. As illustrated in FIG. 4, the canister system 100 includes a main canister 101, a support screen 102, a dividing wall 103, a fuel vapor inlet 104 from a fuel tank, a vent port 105 opening to an atmosphere, a purge outlet 106 to an engine, an initial adsorbent volume 201 in the main canister 101, subsequent adsorbent volumes 202, 203, 204 in the main canister 101, a supplemental canister 300 that includes a subsequent adsorbent volume 301, and a conduit 107 connecting the main canister 101 to the supplemental canister 300.

When the engine is off, the fuel vapor from a fuel tank enters the canister system 100 through the fuel vapor inlet 104 into the main canister 101. The fuel vapor diffuses through the initial adsorbent volume 201 and then the subsequent adsorbent volumes (202, 203, and 204) in the main canister 101 before entering the supplemental canister 300 via the conduit 107. The fuel vapor diffuses through the subsequent adsorbent volume 301 inside the supplemental canister 300 before being released to the atmosphere through the vent port 105 of the canister system. Once the engine is turned on, ambient air is drawn into the canister system 100 through the vent port 105. The purge air flows through the subsequent adsorbent volume 301 in the supplemental canister 300, the subsequent adsorbent volumes (204, 203, 202) in the main canister 101, and then the initial adsorbent volume 201 in the main canister 101, to desorb the fuel vapor adsorbed on the adsorbent volumes (301, 204, 203, 202, 201) before entering the internal combustion engine through the purge outlet 106.

Similar to the main canister, the supplemental canister of the evaporative emission control canister system may include more than one subsequent adsorbent volume. By way of non-limiting example, the supplemental canister 300 of the evaporative emission control canister system 100 may include subsequent adsorbent volumes 301 and 302, as illustrated in FIG. 5.

Furthermore, the supplemental canister of the evaporative emission control canister system may include an empty volume between the subsequent adsorbent volumes. By way of non-limiting example, the supplemental canister 300 of the evaporative emission control canister system 100 may include subsequent adsorbent volumes (301, 302, and 303) and an empty volume 304 between the subsequent adsorbent volumes 302 and 303 as illustrated in FIG. 6. In a non-limiting example shown in FIG. 7, the supplemental canister 300 of the evaporative emission control canister system 100 may include subsequent adsorbent volumes (301, 302, 303), an empty volumes 304 between the subsequent adsorbent volumes 301 and 302, and an empty volumes 305 between the subsequent adsorbent volumes 302 and 303. As previously discussed, the term “empty volume” refers to a volume not including any adsorbent. Such volume may comprise any non-adsorbent including, but not limited to, air gap, foam spacer, screen, conduit, or combinations thereof.

Additionally, the evaporative emission control canister system may include an empty volume between the main canister and the supplemental canister.

When desired, the evaporative emission control canister system may include more than one supplemental canister. The evaporative emission control canister system may further include one or more empty volumes between the main canister and a first supplemental canister, between the supplement canisters, and/or at the end of the last supplemental canister. By way of non-limiting example, the evaporative emission control canister system may include a main canister, a first supplemental canister, a second supplemental canister, a third supplemental canister, an empty volume between the main canister and a first supplemental canister, an empty volume between the first and second supplemental canister, and an empty volume at the end of the third supplemental canister.

As discussed above, FIGS. 1-7 are merely exemplary embodiments of the disclosed evaporative emission control canister system, and those skilled in the art may envision additional embodiments without departing from the scope of the present disclosure.

When desired, the total adsorbent volume (i.e., the sum of the initial adsorbent volume and the subsequent adsorbent volumes) may be the same as the volume of the evaporative emission control canister system. Alternatively, the total adsorbent volume may be less than the volume of the evaporative emission control canister system.

In a particular embodiment, a method of reducing fuel vapor emissions in an evaporative emission control system comprises contacting the fuel vapor with an initial adsorbent volume having an effective incremental adsorption capacity at 25° C. of greater than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane, and with at least one subsequent adsorbent volume having an effective incremental adsorption capacity at 25° C. of less than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane, an effective butane working capacity (BWC) of less than 3 g/dL, and a g-total BWC of between 2 grams and 6 grams. The initial adsorbent volume and the at least one subsequent adsorbent volume are located within a single canister, or the initial adsorbent volume and the at least one subsequent adsorbent volume are located in separate canisters that are connected to permit sequential contact by fuel vapor. The method of reducing fuel vapor emissions has a two-day diurnal breathing loss (DBL) emissions of no more than 20 mg at no more than about 210 liters of purge applied after the 40 g/hr butane loading step.

The term “adsorbent component” or “adsorbent volume,” as used herein, refers to an adsorbent material or adsorbent containing material along vapor flow path, and may consist of a bed of particulate material, a monolith, honeycomb, sheet or other material.

The term “nominal volume,” as used herein, refers to a sum of the volumes of the adsorbent components, and does not include the volumes of gaps, voids, ducts, conduits, tubing, plenum spaces or other volumes along lengths of the vapor flow path that are devoid of adsorbent material across the plane perpendicular to vapor flow path. For example, in FIG. 1 the total nominal volume of the canister system is the sum of the volumes of adsorbent volumes 201 and 202. For example, in FIGS. 2 and 3, the total nominal volume of the canister system is the sum of the volumes of adsorbent volumes 201, 202, 203, and 204. In FIG. 4, the total nominal volume of the canister system is the sum of the volumes of adsorbent volumes 201, 202, 203, 204, and 301. In FIG. 5, the total nominal volume of the canister system is the sum of the volumes of adsorbent volumes 201, 202, 203, 204, 301, and 302. In FIGS. 6 and 7, the total nominal volume of the canister system is the sum of the volumes of adsorbent volumes 201, 202, 203, 204, 301, 302, and 303.

Determination of Nominal Volume Apparent Density

The term “nominal volume apparent density,” as used herein, is the mass of the representative adsorbent in the adsorbent volume divided by the nominal volume of adsorbent, where the length of the volume is defined as the in situ distance within the canister system between the perpendicular plane of the vapor flow path initially in contact with the adsorbent component and the perpendicular plan of the vapor flow path exiting the adsorbent component.

Non-limiting examples of how to calculate the nominal volume apparent density for various forms of adsorbents are described herein.

(A) Granular, Pelletized, or Spherical Adsorbents of Uniform Adsorptive Capacity Across the Length of the Adsorbent Component Flow Path

The standard method ASTM D 2854 (hereinafter “the Standard Method”) may be used to determine the nominal volume apparent density of particulate adsorbents, such as granular and pelletized adsorbents of the size and shape typically used for evaporative emission control for fuel systems. The Standard Method may be used to determine the apparent density of adsorbent volume, when it provides the same apparent density value as the ratio of the mass and the nominal volume of the adsorbent bed found in the canister system. The mass of the adsorbent by the Standard Method is of the representative adsorbent used in the incremental adsorption analysis, i.e., equivalently including or excluding inert binders, fillers, and structural components within the adsorbent volume depending on what representative material is analyzed as the adsorbent sample.

Furthermore, the nominal volume apparent density of adsorbent volume may be determined using an alternative apparent density method, as defined below. The alternative method may be applied to nominal adsorbent volumes that have apparent densities that are not comparably or suitably measured by the Standard Method. Additionally, the alternative apparent density method may be applied to particulate adsorbents in lieu of the Standard Method, due to its universal applicability. The alternative method may be applied to the adsorbent volume that may contain particulate adsorbents, non-particulate adsorbents, and adsorbents of any form augmented by spacers, voids, voidage additives within a volume or sequential similar adsorbent volumes for the effect of net reduced incremental volumetric capacity.

In the alternative apparent density method, the apparent density of adsorbent volume is obtained by dividing the mass of adsorbent by the volume of adsorbent, wherein:

(1) the dry mass basis of the representative adsorbent in the adsorbent volume is measured. For example, a 0.200 g representative sample of the 25.0 g total adsorbent mass in an adsorbent volume is measured for adsorptive capacity by the McBain method. Whereas the McBain method yields an adsorption value of g-butane per g-adsorbent, the applicable mass is 25.0 g for the numerator in the apparent density of the adsorbent volume that then allows conversion of the McBain analytical value to the volumetric property of the adsorbent volume; and

(2) the volume of the adsorbent component in the denominator of the apparent density is defined as the in situ geometric volume under which the superficial vapor flow path occurs within the canister system. The length of the volume is bounded by a plane perpendicular to the superficial vapor flow entrance of the adsorbent volume in question (i.e., the point at which there is adsorbent present on the perpendicular plane) and a plane perpendicular to the superficial flow at the vapor flow exit of the adsorbent volume in question (i.e., the point at which there is no adsorbent across the plane perpendicular to vapor flow).

(B) Honeycombs, Monolith, or Foam Adsorbents

(1) Cylindrical Honeycomb Adsorbents

The apparent density of cylindrical honeycomb absorbents may be determined according to the procedure of Purification Cellutions, LLC (Waynesboro, Ga.) SOP 500-115. The volume of adsorbent is a multiple of the cross-sectional area (A) and the length (h) of the adsorbent. The length (h) of the adsorbent is defined as the distance between the front plane of the adsorbent perpendicular to vapor or gas flow entering the adsorbent and the back plane of the adsorbent where the vapor or gas exits the adsorbent. The volume measurement is that of the nominal volume, which is also used for defining bed volume ratios for purge. In the case of a cylindrical honeycomb adsorbent of circular cross-section, the adsorbent cross-sectional area is determined by πd²/4, where d is the average diameter measured at four points on each end of the honeycomb. The nominal adsorbent volume and the nominal volume apparent density are calculated as follows:

Nominal Adsorbent Volume=h×A

Nominal Volume Apparent Density=Part Mass/(h×A)

wherein “Part Mass” is the mass of the adsorbent for which a representative adsorbent sample was tested for adsorptive properties, including representative proportions of inert or adsorptive binders and fillers.

By way of non-limiting examples, FIG. 9 shows the boundary definitions for the nominal volume of a honeycomb adsorbent 109 having a cross-sectional area A. The vapor or gas flows through the honeycomb adsorbent 109 in the direction of D1 to D2. The vapor or gas enters the front plane (F) of the adsorbent 109, flows through the length (h) of the adsorbent 109, and exits back plane (B) of the adsorbent 109. The nominal volume of a honeycomb adsorbent 109 equals to the cross-sectional area A×the length h. Similarly, FIG. 10 shows the boundary definitions for the nominal volume of foam adsorbent 110.

(2) Pleated, Corrugated and Sheet Adsorbents

For pleated and corrugated adsorbents, the nominal adsorbent volume includes all the void space created by the pleats and corrugations. The volume measurement is that of the nominal volume, which is also used for defining bed volume ratios for purge. The nominal volume and the apparent density of adsorbent are calculated as follows:

Nominal Adsorbent Volume=h×A

Nominal Volume Apparent Density=Part Mass/(h×A)

wherein

“Part Mass” is the mass of the adsorbent for which a representative adsorbent sample was tested for adsorptive properties, including representative proportions of inert or adsorptive binders and fillers,

h is the length of adsorbent, defined as the distance between the front plane of the adsorbent perpendicular to vapor or gas flow entering the filter and the back plane of the adsorbent where the vapor or gas exits the filter, and

A is the cross-sectional area of adsorbent.

By way of non-limiting example, FIG. 11 shows the boundary definitions for the volume of a stacked corrugated sheet adsorbent monolith 111. It is also within those skilled in the art to form such a monolith as an extruded honeycomb.

In the case of a pleated adsorbent, the adsorbent cross-sectional area is determined by L×W, where L is the distance from one edge of the adsorbent to the opposite edge of the adsorbent in direction X, and W is the distance from one edge of the adsorbent to the opposite edge of the adsorbent in direction Y.

By way of non-limiting examples, FIG. 12 shows the boundary definitions for the volume of a single pleat or corrugation 112. FIG. 13 shows the boundary definitions for the volume of a pleated or corrugated sheet 113 with vapor flow path provided through the sheet by some form of permeability to gas flow. The face of the sheet is perpendicular to the vapor flow. In contrast, FIG. 14 shows the boundary definitions for the volume of a pleated or corrugated sheet 114 where its face is angled to gas flow. FIG. 15 shows the boundary definitions for the volume of an adsorbent volume 115 of parallel adsorbent sheets. FIG. 16 shows the boundary definitions for the volume of an adsorbent sleeve 116.

Determination of Nominal Incremental Adsorption Capacity

The term “nominal incremental adsorption capacity,” as used herein, refers to an adsorption capacity according to the following equation:

Nominal Incremental Adsorption Capacity=[Adsorbed Butane at 50 vol %−Adsorbed Butane at 5 vol %]×Nominal Volume Apparent Density×1000

wherein

“Adsorbed Butane at 50 vol %” is the gram mass of absorbed n-butane per gram mass of adsorbent sample at 50 vol % butane concentration;

“Adsorbed Butane at 5 vol %” is the gram mass of absorbed n-butane per gram mass of adsorbent sample at 5 vol % butane concentration; and

“Nominal Volume Apparent Density” is as defined previously.

Determination of the Nominal Volume Butane Working Capacity (BWC)

The standard method ASTM D5228 may be used to determine the nominal volume butane working capacity (BWC) of the adsorbent volumes containing particulate granular and/or pelletized adsorbents.

A modified version of ASTM D5228 method may be used to determine the nominal volume butane working capacity (BWC) of the honeycomb, monolith, and/or sheet adsorbent volumes. The modified method may also be used for particulate adsorbents, where the particulate adsorbents include fillers, voids, structural components, or additives. Furthermore, the modified method may be used where the particulate adsorbents are not compatible with the standard method ASTM D5228, e.g., a representative adsorbent sample may not be readily placed as the 16.7 mL fill in the sample tube of the test.

The modified version of ASTM D5228 method is as follows. The adsorbent sample is oven-dried for a minimum of eight hours at 110±5° C., and then placed in desiccators to cool down. The dry mass of the adsorbent sample is recorded. The mass of the empty testing assembly is determined before the adsorbent sample is assembled into a testing assembly. Then, the test assembly is installed into the a flow apparatus and loaded with n-butane gas for a minimum of 25 minutes (±0.2 min) at a butane flow rate of 500 ml/min at 25° C. and 1 atm pressure. The test assembly is then removed from the BWC test apparatus. The mass of the test assembly is measured and recorded to the nearest 0.001 grams. This n-butane loading step is repeated for successive 5 minutes flow intervals until constant mass is achieved. For example, the total butane load time for a 35 mm diameter×150 mm long honeycomb (EXAMPLE 2 Adsorbent 1) was 66 minutes. The test assembly may be a holder for a honeycomb or monolith part, for the cases where the nominal volume may be removed and tested intact. Alternatively, the nominal volume may need to be a section of the canister system, or a suitable reconstruction of the nominal volume with the contents appropriately oriented to the gas flows, as otherwise encountered in the canister system.

The test assembly is reinstalled to the test apparatus and purged with 2.00 liter/min air at 25° C. and 1 atm pressure for a set selected purge time (±0.2 min) according to the formula: Purge Time (min)=(719×Nominal Volume (cc))/(2000 (cc/min)).

The direction of the air purge flow in the BWC test is in the same direction as the purge flow to be applied in the canister system. After the purge step, the test assembly is removed from the BWC test apparatus. The mass of the test assembly is measured and recorded to the nearest 0.001 grams within 15 minutes of test completion.

The nominal volume butane working capacity (BWC) of the adsorbent sample was determined using the following equation:

${{Nominal}\mspace{14mu} {Volume}\mspace{14mu} {BWC}\mspace{14mu} \left( {g\text{/}{dL}} \right)} = \frac{{Amount}\mspace{14mu} {of}\mspace{14mu} {Butane}\mspace{14mu} {Purged}\mspace{14mu} (g)}{{Nominal}\mspace{14mu} {Adsorbent}\mspace{14mu} {Volume}\mspace{14mu} ({dL})}$

wherein

“Nominal Volume Apparent Density” is as defined previously, and

Amount of Butane Purged=Mass of the test assembly after loading−Mass of the test assembly after purge.

The term “g-total BWC,” as used herein, refers to g-amount of butane purged.

Determination of Effective Volumetric Properties

The effective volume of adsorbents takes into account the air gaps, voids and other volumes between the nominal volumes of adsorbents along the vapor flow path that lack adsorbent. Thus, the effective volumetric properties of adsorbent refer to the properties of the adsorbent that take into account air gaps, voids and other volumes between the nominal volumes of adsorbents that lack adsorbent along the vapor flow path.

The effective volume (V_(eff)) for a given length of the vapor flow path is the sum of the nominal volumes of adsorbent (V_(nom, i)) present along that vapor path length plus adsorbent-free volumes along that vapor flow path (V_(gap, j)).

V _(eff) =ΣV _(nom,i) +V _(gap,j)

A volumetric adsorptive properties of an effective volume (B_(eff)), such as incremental adsorption capacity (g/L), apparent density (g/mL) and BWC (g/dL), is the sum of each property of the individual nominal volumes to be considered as part of the effective volume (B_(nom, i)) multiplied by each individual nominal volume (V_(nom, i)), then divided by the total effective volume (V_(eff)):

B _(eff)=Σ(B _(nom,i) ×V _(nom,i))/V _(eff)

Thus, the term “effective incremental adsorption capacity” is the sum of each nominal incremental adsorption capacity multiplied by each individual nominal volume, and then divided by the total effective volume.

The term “effective butane working capacity (BWC)” is the sum of each BWC value multiplied by each individual nominal volume, and then divided by the total effective volume.

The term “effective apparent density” is the sum of each apparent density multiplied by each individual nominal volume, and then divided by the total effective volume

The term “g-total BWC of the effective volume” is the sum of the g-total BWC gram values of the nominal volumes within the effective volume.

As non-limiting examples of how to determine effective volume of adsorbents, FIG. 17 shows the effective volume for three adsorbent honeycomb nominal volumes connected in the flow path by gaps of equal cross-sectional areas, with the arrow in the direction of D1 to D2 indicating vapor flow into the effective volume, towards the canister system vent. FIG. 18 shows three adsorbent honeycomb nominal volumes connected by conduit sections of different cross-sectional areas compared with the honeycomb cross-sectional areas. In FIGS. 17 and 18, the honeycomb nominal volumes and the gaps appear symmetric. However, it is understood that the honeycomb nominal volumes and the gaps may have different dimensions.

In some embodiments, the volumetric adsorptive properties of the adsorbent volumes may be deceased along the vapor flow path. By way of non-limiting example, the volumetric incremental capacity and butane working capacity (BWC) of the adsorbent volumes may be decreased towards the vent direction of the canister system. The diminished volumetric adsorptive properties may be attained by modifying the properties of the separate sections of adsorbent, by varying the size of the gaps between adsorbent nominal volumes (FIG. 19), by adjusting the dimensions of individual adsorbent nominal volumes, separately (FIGS. 20 and 21), or by a combination thereof (FIG. 22). By way of non-limiting examples, as shown in FIGS. 20 and 21, the canister system (120, 121) may include adsorbent volume sections “F,” “M,” and “B” along the flow path in the direction of D1 to D2. The effective butane working capacities (BWC) of the adsorbent volume sections may be decreased along the flow path in the direction of D1 to D2 (i.e., the effective BWC of the adsorbent volume section F>the effective BWC of the adsorbent volume section M>the effective BWC of the adsorbent volume section B). In some embodiments, the effective BWC of the adsorbent volume section M and/or section B may be less than 3 g/dL, while the effective BWC of the canister system may be more than or equal to 3 g/dl.

In a particular embodiment, the evaporative emission control system include: a fuel tank for storing fuel; an engine having an air induction system and adapted to consume the fuel; an evaporative emission control canister system comprising one or more canister(s); a fuel vapor inlet conduit from the fuel tank to the canister system; a fuel vapor purge conduit from the canister system to the air induction system of the engine; and a vent conduit for venting the canister system when the engine is off and for admission of purge air to the canister system when the engine is on. The evaporative emission control canister system is defined by a fuel vapor flow path from the fuel vapor inlet conduit to the initial adsorbent volume toward the at least one subsequent adsorbent volume and the vent conduit, and by an air flow path from the vent conduit to the at least one subsequent adsorbent volume toward the initial adsorbent volume and the fuel vapor purge conduit. The evaporative emission control canister system includes an initial adsorbent volume having an effective incremental adsorption capacity at 25° C. of greater than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane; and at least one subsequent adsorbent volume having an effective incremental adsorption capacity at 25° C. of less than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane, an effective butane working capacity (BWC) of less than 3 g/dL, and a g-total BWC of between 2 grams and 6 grams. The initial adsorbent volume and the at least one subsequent adsorbent volume are located within a single canister, or the initial adsorbent volume and the at least one subsequent adsorbent volume are located in separate canisters that are connected to permit sequential contact by fuel vapor. The evaporative emission control canister system has a two-day diurnal breathing loss (DBL) emissions of no more than 20 mg at no more than about 210 liters of purge applied after the 40 g/hr butane loading step.

The disclosed evaporative emission control system may provide low diurnal breathing loss (DBL) emissions even under a low purge condition. The evaporative emission performance of the disclosed evaporative emission control system may be within the regulation limits defined by the California Bleed Emissions Test Procedure (BETP), which is 20 mg or less, even under a low purge condition.

The term “low purge,” as used herein, refers to a purge level at or below 210 liters applied after the 40 g/hr butane loading step (i.e., 100 bed volumes for a 2.1 liter adsorbent component system).

The evaporative emission control system may provide low diurnal breathing loss (DBL) emissions even when being purged at or below 210 liters applied after the 40 g/hr butane loading step. In some embodiments, the evaporative emission control system may be purged at or below 157.5 liters applied after the 40 g/hr butane loading step.

The evaporative emission control system may provide low diurnal breathing loss (DBL) emissions even when being purged at or below 100 BV (bed volumes based on a 2.1 liter nominal volume of the canister system) applied after the 40 g/hr butane loading step. In some embodiments, the evaporative emission control system may be purged at or below 75 BV (based on a 2.1 liter nominal volume of the canister system) applied after the 40 g/hr butane loading step.

In some embodiments, the evaporative emission control system may include a heat unit to further enhance the purge efficiency. By way of non-limiting example, the evaporative emission control system may include a heat unit for heating the purge air, at least one subsequent adsorbent volume, or both.

The adsorbents suitable for use in the adsorbent volumes may be derived from many different materials and in various forms. It may be a single component or a blend of different components. Furthermore, the adsorbent (either as a single component or a blend of different components) may include a volumetric diluent. Non-limiting examples of the volumetric diluents may include, but are not limited to, spacer, inert gap, foams, fibers, springs, or combinations thereof.

Any known adsorbent materials may be used including, but not limited to, activated carbon, carbon charcoal, zeolites, clays, porous polymers, porous alumina, porous silica, molecular sieves, kaolin, titania, ceria, or combinations thereof. Activated carbon may be derived from various carbon precursors. By way of non-limiting example, the carbon precursors may be wood, wood dust, wood flour, cotton linters, peat, coal, coconut, lignite, carbohydrates, petroleum pitch, petroleum coke, coal tar pitch, fruit pits, fruit stones, nut shells, nut pits, sawdust, palm, vegetables such as rice hull or straw, synthetic polymer, natural polymer, lignocellulosic material, or combinations thereof. Furthermore, activated carbon may be produced using a variety of processes including, but are not limited to, chemical activation, thermal activation, or combinations thereof.

A variety of adsorbent forms may be used. Non-limiting examples of the adsorbent forms may include granular, pellet, spherical, honeycomb, monolith, pelletized cylindrical, particulate media of uniform shape, particulate media of non-uniform shape, structured media of extruded form, structured media of wound form, structured media of folded form, structured media of pleated form, structured media of corrugated form, structured media of poured form, structured media of bonded form, non-wovens, wovens, sheet, paper, foam, or combinations thereof. The adsorbent (either as a single component or a blend of different components) may include a volumetric diluent. Non-limiting examples of the volumetric diluents may include, but are not limited to, spacer, inert gap, foams, fibers, springs, or combinations thereof. Furthermore, the adsorbents may be extruded into special thin-walled cross-sectional shapes, such as hollow-cylinder, star, twisted spiral, asterisk, configured ribbons, or other shapes within the technical capabilities of the art. In shaping, inorganic and/or organic binders may be used.

The honeycomb adsorbents may be in any geometrical shape including, but are not limited to, round, cylindrical, or square. Furthermore, the cells of honeycomb adsorbents may be of any geometry. Honeycombs of uniform cross-sectional areas for the flow-through passages, such as square honeycombs with square cross-sectional cells or spiral wound honeycombs of corrugated form, may perform better than round honeycombs with square cross-sectional cells in a right angled matrix that provides adjacent passages with a range of cross-sectional areas and therefore passages that are not equivalently purged. Without being bound by any theory, it is believed that the more uniform cell cross-sectional areas across the honeycomb faces, the more uniform flow distribution within the part during both adsorption and purge cycles, and, therefore, lower DBL emissions from the canister system.

In some embodiments, the evaporative emission control system may further include one or more heat input unit(s) for heating one or more adsorbent volume(s) and/or one or more empty volume(s). The heat input units may include, but are not limited to, internal resistive elements, external resistive elements, or heat input units associated with the adsorbent. The heat input unit associated with the adsorbent may be an element separate from the adsorbent (i.e., non-contacted with adsorbents). Alternatively, the heat input unit associated with the adsorbent may be a substrate or layer on to which the adsorbent is attached, bonded, non-bonded, or in physical contact. The heat input unit associated with the adsorbent may be adsorbent directly heated electrically by having appropriate resistivity. The resistivity properties of the adsorbent may be modified by the addition of conductive or resistive additives and binders in the original preparation of the adsorbent and/or in the forming of the adsorbent into particulate or monolithic forms. The conductive component may be conductive adsorbents, conductive substrates, conductive additives and/or conductive binders. The conductive material may be added in adsorbent preparation, added in intermediate shaping process, and/or added in adsorbent shaping into final form. Any mode of heat input unit may be used. By way of non-limiting example, the heat input unit may include a heat transfer fluid, a heat exchanger, a heat conductive element, and positive temperature coefficient materials. The heat input unit may or may not be uniform along the heated fluid path length (i.e., provide different local intensities). Furthermore, the heat input unit may or may not be distributed for greater intensity and duration of heating at different points along the heated fluid path length.

Examples

Determination of Incremental Adsorption Capacity

FIG. 8 shows a simplified schematic drawing of the apparatus used for the determination of the butane adsorption capacity. This is known in the field as the McBain method. The apparatus 800 includes a sample pan 801 and a spring 802 inside a sample tube 803, a rough vacuum pump 804, a diffusion pump 805, a stopcock 806, metal/O-ring vacuum valves 807-809, a butane cylinder 810, a pressure readout unit 811, and at least one conduit 812 connecting the components of the apparatus 800.

The representative adsorbent component sample (“adsorbent sample”) was oven-dried for more than 3 hours at 110° C. before loading onto the sample pan 801 attached to the spring 802 inside the sample tube 803. Then, the sample tube 803 was installed into the apparatus 800. The adsorbent sample shall include representative amounts of any inert binders, fillers and structural components present in the nominal volume of the adsorbent component when the Apparent Density value determination equivalently includes the mass of the inert binders, fillers, and structural components in its mass numerator. Conversely, the adsorbent sample shall exclude these inert binders, fillers, and structural components when the Apparent Density value equivalently excludes the mass of the inert binders, fillers, and structural components in its numerator. The universal concept is to accurately define the adsorptive properties for butane on a volume basis within the nominal volume.

A vacuum of less than 1 torr was applied to the sample tube, and the adsorbent sample was heated at 105° C. for 1 hour. The mass of the adsorbent sample was then determined by the extension amount of the spring using a cathetometer. After that, the sample tube was immersed in a temperature-controlled water bath at 25° C. Air was pumped out of the sample tube until the pressure inside the sample tube was 10⁻⁴ torr. n-Butane was introduced into the sample tube until equilibrium was reached at a selected pressure. The tests were performed for two data sets of four selected equilibrium pressures each, taken about 38 torr and taken about 380 torr. The concentration of n-butane was based on the equilibrium pressure inside the sample tube. After each test at the selected equilibrium pressure, the mass of the adsorbent sample was measured based on the extension amount of the spring using cathetometer. The increased mass of the adsorbent sample was the amount of n-butane adsorbed by the adsorbent sample. The mass of n-butane absorbed (in gram) per the mass of the adsorbent sample (in gram) was determined for each test at different n-butane equilibrium pressures and plotted in a graph as a function of the concentration of n-butane (in % volume). A 5 vol % n-butane concentration (in volume) at one atmosphere is provided by the equilibrium pressure inside the sample tube of 38 torr. A 50 vol % n-butane concentration at one atmosphere is provided by the equilibrium pressure inside the sample tube of 380 torr. Because equilibration at precisely 38 torr and 380 torr may not be readily obtained, the mass of adsorbed n-butane per mass of the adsorbent sample at 5 vol % n-butane concentration and at 50 vol % n-butane concentration were interpolated from the graph using the data points collected about the target 38 and 380 torr pressures.

Alternatively, Micromeritics (such as Micromeritics ASAP 2020) may be used for determining the incremental butane adsorption capacity instead of the McBain method.

Determination of Diurnal Breathing Loss (DBL) Emissions

The evaporative emission control systems of EXAMPLES 1-13 (identified below) were assembled with the selected amounts and types of adsorbents as shown in TABLES 1-3.

Each example was uniformly preconditioned (aged) by repetitive cycling of gasoline vapor adsorption using certified TF-1 fuel (9 RVP, 10 vol % ethanol) and 300 nominal bed volumes of dry air purge at 22.7 LPM based on the main canister (e.g., 630 liters for a 2.1 L main canister and 450 liters for a 1.5 L main canister). The gasoline vapor load rate was 40 g/hr and the hydrocarbon composition was 50 vol %, generated by heating two liters of gasoline to about 36° C. and bubbling air through at 200 ml/min. The two-liter aliquot of fuel was replaced automatically with fresh gasoline every two hours until 5000 ppm breakthrough was detected by a FID (flame ionization detector). A minimum of 25 aging cycles were used on a virgin canister. The aging cycles were followed by a single butane adsorption/air purge step. This step was to load butane at 40 g/hour at a 50 vol % concentration in air at one atm to 5000 ppm breakthrough, soak for one hour, then purge with dry air for 21 minutes with a total purge volume attained by selecting the appropriate constant air purge rate for that period. The canister was then soaked with the ports sealed for 24 hour at 20° C.

The DBL emissions were subsequently generated by attaching the tank port of the example to a fuel tank filled 40 vol % (based on its rated volume) with CARB Phase II fuel (7 RVP, 0% ethanol). Prior to attachment, the filled fuel tank had been stabilized at 18.3° C. for 24 hours while venting. The tank and the example were then temperature-cycled per CARB's two-day temperature profile, each day from 18.3° C. to 40.6° C. over 11 hours, then back down to 18.3° C. over 13 hours. Emission samples were collected from the example vent at 5.5 hours and 11 hours during the heat-up stage into Kynar bags. The Kynar bags were filled with nitrogen to a known total volume based on pressure and then evacuated into a FID to determine hydrocarbon concentration. The FID was calibrated with a 5000 ppm butane standard. From the Kynar bag volume, the emissions concentration, and assuming an ideal gas, the mass of emissions (as butane) was calculated. For each day, the mass of emissions at 5.5 hours and 11 hours were added. Following CARB's protocol the day with the highest total emissions was reported as “2-day emissions.” In all cases, the highest emissions were on Day 2. This procedure is generally described in SAE Technical Paper 2001-01-0733, titled “Impact and Control of Canister Bleed Emissions,” by R. S. Williams and C. R. Clontz, and in CARB's LEV III BETP procedure (section D.12 in California Evaporative Emissions Standards and Test Procedures for 2001 and Subsequent Model Motor Vehicles, Mar. 22, 2012).

For EXAMPLES 1-4, 13 and EXAMPLES 7-8, a 68 L fuel tank and a 2.1 liter main canister (TABLE 1, Main Canister Type #1) was used as a main canister having fuel-source side volumes (i.e., an initial adsorbent volume) filled with 1.8 liters of NUCHAR® BAX 1500 activated carbon adsorbent and a vent-side volume filled with 0.3 liters of NUCHAR® BAX LBE activated carbon adsorbent. The volumes were configured such that there was a 1500 ml fuel-source side chamber and a 600 ml vent-side chamber, where the fuel-source chamber had a cross sectional area (CSA) that was 2.5 times the vent-side CSA. The BAX 1500 activated carbon filled the fuel source chamber (similar to volumes 201 plus 202 in FIGS. 2-7) and 300 mL of the immediate downstream volume in the vent-side chamber (similar to volume 203 in FIGS. 2-7). The 300 mL of the BAX LBE activated carbon filled the remaining volume of the vent-side chamber (similar to volume 204 in FIG. 7). NUCHAR® BAX 1500 activated and NUCHAR® BAX LBE activated carbon are wood-based activated carbon products, commercially available from MeadWestvaco Corporation, having an incremental adsorption capacity at 25° C. of 80 grams n-butane/L and 24 grams n-butane/L respectively, between vapor concentration of 5 vol % and 50 vol % n-butane (“Nominal Incremental Capacity” in TABLE 1). For the post-butane loading air purge step, each canister system in EXAMPLES 1-4, 13 and EXAMPLES 7-8 was purged with 157.5 liters of purge air at a purge rate of 7.5 lpm. In terms of bed volume ratios of purge volume divided by the total nominal volume of the canister systems, the purge applied was between 66.0 and 75.0 bed volumes (BV).

For EXAMPLES 5-6 and 9-12, a 45 L fuel tank and a 1.5 liter main canister (TABLE 1, Main Canister Type #2) was used as a main canister having fuel-source side volumes (i.e., an initial adsorbent volume) filled with 1.2 liters of NUCHAR® BAX 1100 activated carbon adsorbent and a vent-side volume filled with 0.3 liters of NUCHAR® BAX LBE activated carbon adsorbent. The volumes were configured such that there was a 1000 ml fuel-source side chamber and a 500 ml vent-side chamber, where the fuel-source chamber had a cross sectional area (CSA) that was 2.0 times the vent-side CSA. The BAX 1100 activated carbon filled the fuel source chamber (similar to volumes 201 plus 202 in FIGS. 2-7) and 200 mL of the immediate downstream volume in the vent-side chamber (similar to volume 203 in FIGS. 2-7). The 300 mL of the BAX LBE activated carbon filled the remaining volume of the vent-side chamber (similar to volume 204 in FIG. 7). NUCHAR® BAX 1100 activated is a wood-based activated carbon product, commercially available from MeadWestvaco Corporation, having an incremental adsorption capacity at 25° C. of 52 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane. During the post-butane loading air purge step, each canister system example was purged with either 100 or 150 liters of purge air at a purge rate of 4.76 or 7.14 lpm, respectively. In terms of bed volume ratios of purge volume divided by the total nominal volume of the canister systems, the purge applied was between 55.9 and 91.2 BV.

EXAMPLES 1-13 each included none, one, or two additional vent-side adsorbent volumes in-series. The first supplemental canister downstream along the vapor flow path from the main canister (if present) was noted as “Adsorbent 1” and a second in-series supplemental canister (if present) downstream along the vapor flow path from Adsorbent 1 was noted as “Adsorbent 2.” One type of additional vent-side adsorbent (similar to supplemental canister 300 in FIG. 4) was described as “35×150,” which was a 35 mm diameter×150 mm long, 200 cells per square inch (cpsi) cylindrical carbon honeycomb. The accounting of the effective volume for the “35×150” adsorbent was the same boundaries as shown in FIG. 9, that is, the effective volume was bounded by the vapor entrance and exit faces of the honeycomb, and equal to its nominal volume. The second type of additional vent-side adsorbent (similar to supplemental canister 300 in FIG. 7) was described as “3-35×50,” which was three 35 mm diameter×50 mm long, 200 cpsi cylindrical carbon honeycombs, including two 35 mm diameter×7 mm thick foam spacers. Each foam spacer created a 7 mL voidage gap between each sequential 50 mm long honeycomb length, similar to gaps 304 and 305 in FIG. 7. The accounting of the effective volume was the same boundaries as shown in FIG. 17, that is, the effective volume was bounded by the vapor entrance face of the first of the three honeycombs and exit faces of the third of the three honeycombs, and equal to the nominal volumes of the three honeycombs plus the volumes of the 7-mm thick spacers. The nominal incremental adsorption capacity at 25° C. of n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane was shown as the “Nominal Incremental Capacity.” When based on the effective volume, the incremental adsorption capacity at 25° C. of n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane was shown as the “Effective Incremental Capacity.” The two-day DBL emissions were reported as the “2-day DBL Emissions” in units of mg. The reported results were often the average of several replicates of the BETP in order to verify findings.

The evaporative emission control canister system of EXAMPLES 1-4, 13 and EXAMPLES 7-8 each included an initial adsorbent volume of BAX 1500 activated carbon adsorbent having a nominal incremental adsorption capacity at 25° C. of 80 g n-butane/L (i.e., more than 35 g/L) between vapor concentration of 5 vol % and 50 vol % n-butane, and a subsequent adsorbent volume of BAX LBE activated carbon adsorbent having a nominal incremental adsorption capacity at 25° C. of 24 g/L (less than 35 g/L) between vapor concentration of 5 vol % and 50 vol % n-butane (less than 35 g/L). This is main canister type #1 in TABLE 1.

EXAMPLE 1 was the evaporative emission control canister system disclosed in the U.S. Pat. No. RE38,844. As shown in TABLE 2, the evaporative emission control canister system of EXAMPLE 1 provided a 2-day DBL Emissions of 215 mg under a low purge condition of 75 bed volume (BV) of purge air after butane loading (i.e., 157.5 liters). These 2-day DBL Emissions were more than an order of magnitude above the 20 mg regulation limit under the California Bleed Emissions Test Procedure (BETP). Thus, the 20 mg regulation limits under the California Bleed Emissions Test Procedure (BETP) could not be achieved by the evaporative emission control canister system disclosed in the U.S. Pat. No. RE38,844.

For EXAMPLE 2, an additional vent-side adsorbent volume (Adsorbent 1) was added to EXAMPLE 1 in the form of an activated carbon honeycomb (“35×150”) having an effective incremental adsorption capacity at 25° C. of 16 g/L (less than 35 g/L) between vapor concentration of 5 vol % and 50 vol % n-butane (less than 35 g/L), an effective BWC of 4.2 g/dL and a g-total BWC of 6.1 g. As shown in TABLE 2, the 2-day DBL Emissions for EXAMPLE 2 with a low purge level of 157.5 liters (applied after butane loading) was 74 mg, which was still above the 20 mg regulation limit under the California Bleed Emissions Test Procedure (BETP). Thus, at the purge level of 157.5 liters applied after butane loading, the evaporative emission control canister system of the U.S. Pat. No. RE38,844 still could not satisfy the 20 mg regulation limit under BETP even when it was used in combination with the additional vent-side adsorbent volume (Adsorbent 1).

For EXAMPLE 3, a second additional vent-side adsorbent volume in the form of a activated carbon honeycomb (Adsorbent 2) of the same type and properties as Adsorbent 1 (“35×150”) was added to the canister system of EXAMPLE 2. Surprisingly, as shown in TABLE 2, there was only a marginal reduction in the 2-day DBL emissions from the additional vent-side adsorbent volume in EXAMPLE 3, to 70 mg and still above the 20 mg regulation limit under the California Bleed Emissions Test Procedure (BETP).

EXAMPLE 4 was a variation of EXAMPLE 3 in that the activated carbon honeycombs were each divided in to three 50 mm long section with narrow spacers in between. For EXAMPLE 4, the spacers reduced the effective incremental capacities of Adsorbents 1 and 2 to 14.6 g/L and reduced the effective BWC to 3.9 g/dL, but, by definition, kept the g-total BWC the same, at 6.1 g. As shown in TABLE 2, the 2-day DBL emissions of EXAMPLE 4 remained high at 52 mg and were still above the 20 mg regulation limits under the California Bleed Emissions Test Procedure (BETP).

In EXAMPLE 13, Adsorbent 2 was honeycombs divided into two 50 mm long sections with a narrow spacer in between. The effective incremental capacity was 6.1 g/L and the effective BWC was 1.6 g/dL. By definition, the g-total BWC was 1.6 g. As shown in TABLE 2, the 2-day DBL emissions of EXAMPLE 13 remained high at 35 mg and were still above the 20 mg regulation limits under the California Bleed Emissions Test Procedure (BETP).

For EXAMPLE 7, Adsorbent 2 had an effective incremental capacity of 9.8 g/L, an effective BWC of 2.6 g/dL and a g-total BWC of 4.0 g. For EXAMPLE 8, Adsorbent 2 had an effective incremental capacity of 10.7 g/L, an effective BWC of 2.8 g/dL and a g-total BWC of 4.4 g. As shown in TABLE 2, with 157.5 liters of purge, the canister systems of EXAMPLES 7 and 8 provided the 2-day DBL Emissions of 10.3 g/dl and 13 g/dl, respectively. Thus, the canister systems of EXAMPLES 7 and 8 had the 2-day DBL Emissions well below the BETP requirement of less than 20 mg for low purge conditions of 157.5 liters (66.0 BV).

The evaporative emission control canister system of EXAMPLES 5, 6 and 9-12 were based on the main canister type #2 in TABLE 1.

EXAMPLE 12 was the evaporative emission control canister system similar to those disclosed in the U.S. Pat. No. RE38,844. As shown in TABLE 3, the evaporative emission control canister system of EXAMPLE 12 did not include any additional adsorbent volume on the vent side. EXAMPLE 12 provided 2-day DBL Emissions of 175 mg under a low purge condition of 100 bed volume (BV) of purge air after butane loading (i.e., 150 liters), which was about nine time higher than the 20 mg regulation limit under the California Bleed Emissions Test Procedure (BETP). This confirmed that the evaporative emission control canister system similar to those disclosed in the U.S. Pat. No. RE38,844 was not able to achieve the 2-day DBL Emissions requirements under the BETP (i.e., less than 20 mg) when low purge was used.

In EXAMPLE 5, a low volume of purge after butane loading 150 liters was applied, or 91.2 BV for the 1.5 L nominal volume of the canister system that included an additional vent-side adsorbent volume of a “35×150” activated carbon honeycomb as Adsorbent 1. As shown in TABLE 3, the 2-day DBL emissions were high at 57 mg and above the 20 mg regulation limit under the California Bleed Emissions Test Procedure (BETP).

For EXAMPLE 6, the purge applied was reduced to 100 liters, or 55.9 BV for the main canister type #2 that included the same additional vent-side adsorbent volumes as EXAMPLE 4. As shown in TABLE 3, the 2-Day DBL emissions were high at 80 mg and above the 20 mg regulation limits under the California Bleed Emissions Test Procedure (BETP).

The canister systems of EXAMPLES 9, 10 and 11 each included an initial adsorbent volume of NUCHAR® BAX 1100 activated carbon adsorbent having an incremental adsorption capacity at 25° C. of 52 g n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane (i.e., more than 35 g/L) as part of the main canister type #2, and at least one subsequent adsorbent volume (“Adsorbent 2” in TABLE 3) having an effective incremental adsorption capacity at 25° C. butane adsorption capacity of less than 35 g/L between vapor concentration of 5 vol % and 50 vol % n-butane and a g-total BWC of between 2 and 6 g.

Adsorbent 2 in EXAMPLE 9 had an effective incremental capacity of 11.7 g/L, an effective BWC of 3.1 g/dL (greater than 3 g/dL) and a g-total BWC of 4.8 g. As shown in TABLE 3, the 2-day DBL emissions for EXAMPLE 9 under the low purge of 100 liters (i.e., 55.9 BV) were 51 mg and well above the BETP requirement of less than 20 mg.

In contrast, Adsorbent 2 in EXAMPLE 10 had an effective incremental capacity of 9.8 g/L, an effective BWC of 2.6 g/dL (less than 3 g/dL) and a g-total BWC of 4.0 g. As shown in TABLE 3, the 2-day DBL emissions under the low purge of 100 liters, equal to 55.9 BV, were 13.0 mg and within the BETP requirement of less than 20 mg.

Likewise, Adsorbent 2 in EXAMPLE 11 had an effective incremental capacity of 5.9 g/L, an effective BWC of 1.6 g/dL (less than 3 g/dL) and a g-total BWC of 2.4 g. As shown in TABLE 3, the 2-day DBL emissions under the low purge of 150 liters, equal to 83.9 BV, were 7.3 mg and within the BETP requirement of less than 20 mg.

TABLE 4 and TABLE 5 summarized the conditions of the canister systems of EXAMPLES 1-13, and their measured 2-day DBL emissions. The canister systems of EXAMPLES 7, 8, 10 and 11 provided the 2-day DBL emissions of less than 20 mg, as required under the California Bleed Emissions Test Procedure (BETP). The requirement not to exceed 20 mg for BETP under low purge was met by satisfying a window of adsorptive properties by a vent-side volume, where the window was an effective BWC of less than 3 g/dL and a g-total BWC of between 2 g and 6 g. Thus, the means to achieve the BETP emissions requirement under low purge conditions was more than only a reduction in the working capacity or incremental capacity across the vapor flow path of the canister system and specifically of the vent-side adsorbent volume to a prescribed level, but to additionally have sufficient gram working capacity in that vent-side volume to restrain the emissions.

While the present disclosure is susceptible to various modifications and alternative forms, specific embodiments have been shown by way of example in the drawings and have been described in detail herein. However, the present disclosure is not intended to be limited to the particular forms disclosed. Rather, the present disclosure is to cover all modifications, equivalents, and alternatives falling within the scope of the present disclosure as defined by the following appended claims and their legal equivalents.

TABLE 1 Main Canister Type #1 #2 Fuel Side Nominal Volume (mL) 1800 1200 Adsorbent Type BAX 1500 BAX 1100 Nominal Incremental Capacity (g/L) 80 52 Nominal Apparent Density (g/mL) 0.284 0.358 Vent Side Nominal Volume (mL) 300 300 Adsorbent Type BAX LBE BAX LBE Nominal Incremental Capacity (g/L) 24 24 Nominal Apparent Density (g/mL) 0.383 0.383 Fuel Tank Size (rated L) 68 45

TABLE 2 EXAMPLE 1 2 3 4 13 7 8 Main Canister Type #1 #1 #1 #1 #1 #1 #1 Additional Vent Side Adsorbents Volumes: Adsorbent 1 Nominal Volume (mL) None 144 144 144 144 144 144 Adsorbent 1 Type None “35 × 150” “35 × 150” “3-35 × 50” “3-35 × 50” “3-35 × 50” “3-35 × 50” Adsorbent 1 Effective Volume (mL) None 144 144 158 158 158 158 Nominal Incremental Capacity (g/L) — 16.0 16.0 16.0 16.0 16.0 16.0 Effective Incremental Capacity (g/L) — 16.0 16.0 14.6 14.6 14.6 14.6 Nominal Apparent Density (g/mL) — 0.377 0.377 0.377 0.377 0.377 0.377 Effective Apparent Density (g/mL) — 0.377 0.377 0.345 0.345 0.345 0.345 Nominal BWC (g/dL) — 4.2 4.2 4.2 4.2 4.2 4.2 Effective BWC (g/dL) — 4.2 4.2 3.8 3.8 3.8 3.8 g-Total BWC (g) — 6.1 6.1 6.1 6.1 6.1 6.1 Adsorbent 2 Nominal Volume (mL) None None 144 144 96 144 144 Adsorbent 2 Type None None “35 × 150” “3-35 × 50” “2-35 × 50” “3-35 × 50” “3-35 × 50” Adsorbent 2 Effective Volume (mL) None None 144 158 103 158 158 Nominal Incremental Capacity (g/L) — — 16.0 16.0 6.5 10.7 11.7 Effective Incremental Capacity (g/L) — — 16.0 14.6 6.1 9.8 10.7 Nominal Apparent Density (g/mL) — — 0.377 0.377 0.559 0.493 0.487 Effective Apparent Density (g/mL) — — 0.377 0.345 0.522 0.451 0.446 Nominal BWC (g/dL) — — 4.2 4.2 1.7 2.8 3.1 Effective BWC (g/dL) — — 4.2 3.8 1.6 2.6 2.8 g-Total BWC (g) — — 6.1 6.1 1.6 4.0 4.4 Total Nominal Volume of Canister 2.10 2.24 2.39 2.39 2.34 2.39 2.39 System (L) Purge Applied After the 40 g/hr Butane 157.5 157.5 157.5 157.5 157.5 157.5 157.5 Loading Step, liters Purge Applied After the 40 g/hr Butane 75.0 70.2 66.0 66.0 67.3 66.0 66.0 Loading Step, BV 2-Day DBL Emissions, mg 215 74 70 52 35 10.3 13

TABLE 3 EXAMPLE 12 5 6 9 10 11 Main Canister Type #2 #2 #2 #2 #2 #2 Additional Vent Side Adsorbents Volumes: Adsorbent 1 Nominal Volume (mL) None 144 144 144 144 144 Adsorbent 1 Type None “35 × 150” “3-35 × 50” “3-35 × 50” “3-35 × 50” “3-35 × 50” Adsorbent 1 Effective Volume (mL) None 144 158 158 158 158 Nominal Incremental Capacity (g/L) — 16.0 16.0 16.0 16.0 16.0 Effective Incremental Capacity (g/L) — 16.0 14.6 14.6 14.6 14.6 Nominal Apparent Density (g/mL) — 0.377 0.377 0.377 0.377 0.377 Effective Apparent Density (g/mL) — 0.377 0.345 0.345 0.345 0.345 Nominal BWC (g/dL) — 4.2 4.2 4.2 4.2 4.2 Effective BWC (g/dL) — 4.2 3.8 3.8 3.8 3.8 g-Total BWC (g) — 6.1 6.1 6.1 6.1 6.1 Adsorbent 2 Nominal Volume (mL) None None 144 144 144 144 Adsorbent 2 Type None None “3-35 × 50” “3-35 × 50” “3-35 × 50” “3-35 × 50” Adsorbent 2 Effective Volume (mL) None None 158 158 158 158 Nominal Incremental Capacity (g/L) — — 16.0 12.8 10.7 6.5 Effective Incremental Capacity (g/L) — — 14.6 11.7 9.8 5.9 Nominal Apparent Density (g/mL) — — 0.377 0.438 0.493 0.558 Effective Apparent Density (g/mL) — — 0.345 0.399 0.451 0.511 Nominal BWC (g/dL) — — 4.2 3.4 2.8 1.7 Effective BWC (g/dL) — — 3.8 3.1 2.6 1.6 g-Total BWC (g) — — 6.1 4.8 4.0 2.4 Total Nominal Volume of Canister System (L) 1.50 1.64 1.79 1.79 1.79 1.79 Purge Applied After the 40 g/hr Butane 150 150 100 100 100 150 Loading Step, liters Purge Applied After the 40 g/hr Butane 100 91.2 55.9 55.9 55.9 83.9 Loading Step, BV 2-Day DBL Emissions, mg 175 57 80 51 13 7.3

TABLE 4 Main Canister Type #1 EX. 1 EX. 2 EX. 3 EX. 4 EX. 13 EX. 7 EX. 8 Fuel side Effective Incremental Adsorption Capacity, g/L 80 80 80 80 80 80 80 Vent Side Adsorbent Volume #0 Effective Incremental Adsorption Capacity, g/L 24 24 24 24 24 24 24 Effective BWC, g/dL 6.3 6.3 6.3 6.3 6.3 6.3 6.3 g-Total BWC, g 18.9 18.9 18.9 18.9 18.9 18.9 18.9 Adsorbent Volume #1 Effective Incremental Adsorption Capacity, g/L N/A 16.0 16.0 16.0 14.6 14.6 14.6 Effective BWC, g/dL N/A 4.2 4.2 4.2 4.2 3.8 3.8 g-Total BWC, g N/A 6.1 6.1 6.1 6.1 6.1 6.1 Adsorbent Volume #2 Effective Incremental Adsorption Capacity, g/L N/A N/A 16.0 14.6 6.1 7.3 8.0 Effective BWC, g/dL N/A N/A 4.2 3.8 1.6 2.6 2.8 g-Total BWC, g N/A N/A 6.1 6.1 1.6 4.0 4.4 2-Day DBL Emission, mg 215 74 70 52 35 10.3 13

TABLE 5 Main Canister Type #2 EX. 12 EX. 5 EX. 6 EX. 9 EX. 10 EX. 11 Fuel side Effective Incremental Adsorption Capacity, g/L 52 52 52 52 52 52 Vent Side Adsorbent Volume #0 Effective Incremental Adsorption Capacity, g/L 24 24 24 24 24 24 Effective BWC, g/dL 6.3 6.3 6.3 6.3 6.3 6.3 g-Total BWC, g 18.9 18.9 18.9 18.9 18.9 18.9 Adsorbent Volume #1 Effective Incremental Adsorption Capacity, g/L N/A 16.0 14.6 14.6 14.6 14.6 Effective BWC, g/dL N/A 4.2 3.8 3.8 3.8 3.8 g-Total BWC, g N/A 6.1 6.1 6.1 6.1 6.1 Adsorbent Volume #2 Effective Incremental Adsorption Capacity, g/L N/A N/A 14.6 11.7 7.3 2.7 Effective BWC, g/dL N/A N/A 3.8 3.1 2.6 1.6 g-Total BWC, g N/A N/A 6.1 4.8 4.0 2.4 2-Day DBL Emission, mg 175 57 80 51 13 7.3 

1. An evaporative emission control canister system for a hybrid vehicle, including one or more canisters and comprising: a fuel-side adsorbent volume having an effective incremental adsorption capacity at 25° C. of greater than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane; and at least one vent-side subsequent adsorbent volume having an effective incremental adsorption capacity at 25° C. of less than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane, a butane working capacity (BWC) of less than 3 g/dL, and a g-total BWC of ≦6 grams, wherein the fuel-side adsorbent volume having an effective incremental adsorption capacity at 25° C. of greater than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane, and the at least one subsequent adsorbent volume are located within a single canister, or in separate canisters that are connected to permit sequential contact by fuel vapor.
 2. The canister system of claim 1, wherein the canister system has a two-day diurnal breathing loss (DBL) emissions of no more than 20 mg as determined by the 2012 California Bleed Emissions Test Procedure (BETP).
 3. The canister system of claim 2, wherein the two-day DBL is no more than 20 mg at no more than 210 liters of purge applied after a 40 g/hr butane loading step.
 4. The canister system of claim 1 wherein the at least one subsequent adsorbent volume has a g-total BWC of between 2 g and 6 g.
 5. The canister system of claim 1, wherein the at least one subsequent adsorbent volume has an effective incremental adsorption capacity at 25° C. of 24 or less grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane.
 6. The canister system of claim 1, wherein the at least one subsequent adsorbent volume has an effective incremental adsorption capacity at 25° C. of 16 or less grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane.
 7. The canister system of claim 1, further comprising at least one additional subsequent adsorbent volume having an effective incremental adsorption capacity at 25° C. of less than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane.
 8. The canister system of claim 7, wherein the at least one additional subsequent adsorbent volume has a lower effective incremental adsorption capacity relative to the subsequent adsorbent volume that precedes it in the flow path from fuel side to vent side.
 9. The canister system of claim 7, wherein each additional subsequent adsorbent volume has a lower effective incremental adsorption capacity than any preceding subsequent adsorbent volume.
 10. The canister system of claim 7, wherein each additional subsequent adsorbent volume has a gram-total BWC of less than 6 g.
 11. The canister system of claim 10, wherein each additional subsequent adsorbent volume has a lower gram-total BWC relative to the subsequent adsorbent volume that precedes it in the flow path from fuel side to vent side.
 12. The canister system of claim 1, wherein the system further includes at least one heat input unit for heating one or more adsorbent volumes.
 13. The canister system of claim 12, wherein the heat input unit include at least one of an internal resistive element, external resistive element, or heat input unit associated with the adsorbent.
 14. The canister system of claim 12, wherein the heat input unit includes at least one of a heat transfer fluid, a heat exchanger, a heat conductive element, or a positive temperature coefficient material.
 15. The canister system of claim 1, wherein the initial adsorbent volume, subsequent volume or both includes an adsorbent selected from the group consisting of activated carbon, carbon charcoal, zeolites, clays, porous polymers, porous alumina, porous silica, molecular sieves, kaolin, titania, ceria, and combinations thereof.
 16. The canister system of claim 15, wherein the initial adsorbent volume, subsequent volume or both includes an adsorbent selected from the group consisting of activated carbon, carbon charcoal, and combinations thereof.
 17. The canister system of claim 16 wherein the activated carbon is derived from a material including a member selected from the group consisting of wood, wood dust, wood flour, cotton linters, peat, coal, coconut, lignite, carbohydrates, petroleum pitch, petroleum coke, coal tar pitch, fruit pits, fruit stones, nut shells, nut pits, sawdust, palm, vegetables, synthetic polymer, natural polymer, lignocellulosic material, and combinations thereof.
 18. The canister system of claim 17 wherein a form of adsorbent in the initial adsorbent volume, the at least one subsequent adsorbent volume, or both includes a member selected from the group consisting of granular, pellet, spherical, honeycomb, monolith, pelletized cylindrical, particulate media of uniform shape, particulate media of non-uniform shape, structured media of extruded form, structured media of wound form, structured media of folded form, structured media of pleated form, structured media of corrugated form, structured media of poured form, structured media of bonded form, non-wovens, wovens, sheet, paper, foam, hollow-cylinder, star, twisted spiral, asterisk, configured ribbons, and combinations thereof.
 19. The canister system of any of claim 1, wherein the at least one subsequent adsorbent volume includes a volumetric diluent.
 20. The canister system of claim 19, wherein the volumetric diluent includes a member selected from the group consisting of inert spacer particles, trapped air spaces, foams, fibers, screens, and combinations thereof.
 21. The canister system of claim 19, wherein the volumetric diluent includes an adsorbent material formed into a high voidage shape selected from the group consisting of stars, hollow tubes, asterisks, spirals, cylinders, configured ribbons, honeycombs, monoliths, and combinations thereof.
 22. An evaporative emission control canister system, including one or more canisters and comprising: an initial adsorbent volume having an effective incremental adsorption capacity at 25° C. of greater than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane; and at least one subsequent adsorbent volume having an effective incremental adsorption capacity at 25° C. of less than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane, and a g-total BWC of less than 6 grams, wherein the initial adsorbent volume and the at least one subsequent adsorbent volume are located within a single canister, or the initial adsorbent volume and the at least one subsequent adsorbent volume are located in separate canisters that are connected to permit sequential contact by fuel vapor, and wherein the canister system has a two-day diurnal breathing loss (DBL) emissions of no more than 20 mg at no more than about 210 liters of purge applied after the 40 g/hr butane loading step.
 23. The canister system of claim 22, wherein the at least one subsequent adsorbent volume has an effective incremental adsorption capacity at 25° C. of 24 or less grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane.
 24. The canister system of claim 22, wherein the at least one subsequent adsorbent volume has an effective incremental adsorption capacity at 25° C. of 16 or less grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane.
 25. The canister system of claim 22, further comprising at least one additional subsequent adsorbent volume having an effective incremental adsorption capacity at 25° C. of less than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane.
 26. The canister system of claim 25, wherein the at least one additional subsequent adsorbent volume has a lower effective incremental adsorption capacity relative to the subsequent adsorbent volume that precedes it in the flow path from fuel side to vent side.
 27. The canister system of claim 25, wherein each additional subsequent adsorbent volume has a lower effective incremental adsorption capacity than any preceding subsequent adsorbent volume.
 28. The canister system of claim 25, wherein each additional subsequent adsorbent volume has a gram-total BWC of from 2 g to 6 g.
 29. The canister system of claim 25, wherein each additional subsequent adsorbent volume has a lower gram-total BWC relative to the subsequent adsorbent volume that precedes it in the flow path from fuel side to vent side.
 30. The canister system of claim 22, wherein the system further includes at least one heat input unit for heating one or more adsorbent volumes.
 31. The canister system of claim 30, wherein the heat input unit include at least one of an internal resistive element, external resistive element, or heat input unit associated with the adsorbent.
 32. The canister system of claim 30, wherein the heat input unit includes at least one of a heat transfer fluid, a heat exchanger, a heat conductive element, or a positive temperature coefficient material.
 33. The canister system of claim 22, wherein the initial adsorbent volume, subsequent volume or both includes an adsorbent selected from the group consisting of activated carbon, carbon charcoal, zeolites, clays, porous polymers, porous alumina, porous silica, molecular sieves, kaolin, titania, ceria, and combinations thereof.
 34. The canister system of claim 33, wherein the initial adsorbent volume, subsequent volume or both includes an adsorbent selected from the group consisting of activated carbon, carbon charcoal, and combinations thereof.
 35. The canister system of claim 34, wherein the activated carbon is derived from a material including a member selected from the group consisting of wood, wood dust, wood flour, cotton linters, peat, coal, coconut, lignite, carbohydrates, petroleum pitch, petroleum coke, coal tar pitch, fruit pits, fruit stones, nut shells, nut pits, sawdust, palm, vegetables, synthetic polymer, natural polymer, lignocellulosic material, and combinations thereof.
 36. The canister system of claim 22, wherein a form of adsorbent in the initial adsorbent volume, the at least one subsequent adsorbent volume, or both includes a member selected from the group consisting of granular, pellet, spherical, honeycomb, monolith, pelletized cylindrical, particulate media of uniform shape, particulate media of non-uniform shape, structured media of extruded form, structured media of wound form, structured media of folded form, structured media of pleated form, structured media of corrugated form, structured media of poured form, structured media of bonded form, non-wovens, wovens, sheet, paper, foam, hollow-cylinder, star, twisted spiral, asterisk, configured ribbons, and combinations thereof.
 37. The canister system of claim 22, wherein the at least one subsequent adsorbent volume includes a volumetric diluent.
 38. The canister system of claim 37, wherein the volumetric diluent includes a member selected from the group consisting of inert spacer particles, trapped air spaces, foams, fibers, screens, and combinations thereof.
 39. The canister system of claim 37, wherein the volumetric diluent includes an adsorbent material formed into a high voidage shape selected from the group consisting of stars, hollow tubes, asterisks, spirals, cylinders, configured ribbons, honeycombs, monoliths, and combinations thereof.
 40. An evaporative emission control canister system, including one or more canisters and comprising: an initial adsorbent volume having an effective incremental adsorption capacity at 25° C. of greater than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane; at least one subsequent adsorbent volume having an effective incremental adsorption capacity at 25° C. of less than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane, and a g-total BWC of 2-6 grams; and a heat input unit for heating one or more adsorbent volumes, wherein the initial adsorbent volume and the at least one subsequent adsorbent volume are located within a single canister, or the initial adsorbent volume and the at least one subsequent adsorbent volume are located in separate canisters that are connected to permit sequential contact by fuel vapor, wherein the canister system has a two-day diurnal breathing loss (DBL) emissions of no more than 20 mg at no more than about 210 liters of purge applied after the 40 g/hr butane loading step.
 41. The canister system of claim 40, further comprising at least one additional subsequent adsorbent volume having an effective incremental adsorption capacity at 25° C. of less than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane.
 42. The canister system of claim 41, wherein the at least one additional subsequent adsorbent volume has a lower effective incremental adsorption capacity relative to the subsequent adsorbent volume that precedes it in the flow path from fuel side to vent side.
 43. The canister system of claim 41, wherein each additional subsequent adsorbent volume has a lower effective incremental adsorption capacity than any preceding subsequent adsorbent volume.
 44. The canister system of claim 41, wherein each additional subsequent adsorbent volume has a gram-total BWC of between 2 grams and 6 grams.
 45. The canister system of claim 41, wherein each additional subsequent adsorbent volume has a lower gram-total BWC relative to the subsequent adsorbent volume that precedes it in the flow path from fuel side to vent side.
 46. The canister system of claim 40, wherein the initial adsorbent volume, subsequent volume or both includes an adsorbent selected from the group consisting of activated carbon, carbon charcoal, zeolites, clays, porous polymers, porous alumina, porous silica, molecular sieves, kaolin, titania, ceria, and combinations thereof.
 47. The canister system of claim 46, wherein the initial adsorbent volume, subsequent volume or both includes an adsorbent selected from the group consisting of activated carbon, carbon charcoal, and combinations thereof.
 48. The canister system of claim 47, wherein the activated carbon is derived from a material including a member selected from the group consisting of wood, wood dust, wood flour, cotton linters, peat, coal, coconut, lignite, carbohydrates, petroleum pitch, petroleum coke, coal tar pitch, fruit pits, fruit stones, nut shells, nut pits, sawdust, palm, vegetables, synthetic polymer, natural polymer, lignocellulosic material, and combinations thereof.
 49. The canister system of claim 40, wherein a form of adsorbent in the initial adsorbent volume, the at least one subsequent adsorbent volume, or both includes a member selected from the group consisting of granular, pellet, spherical, honeycomb, monolith, pelletized cylindrical, particulate media of uniform shape, particulate media of non-uniform shape, structured media of extruded form, structured media of wound form, structured media of folded form, structured media of pleated form, structured media of corrugated form, structured media of poured form, structured media of bonded form, non-wovens, wovens, sheet, paper, foam, hollow-cylinder, star, twisted spiral, asterisk, configured ribbons, and combinations thereof.
 50. The canister system of claim 40, wherein the at least one subsequent adsorbent volume includes a volumetric diluent.
 51. The canister system of claim 50, wherein the volumetric diluent includes an adsorbent material formed into a high voidage shape selected from the group consisting of stars, hollow tubes, asterisks, spirals, cylinders, configured ribbons, honeycombs, monoliths, and combinations thereof.
 52. An evaporative emission control canister system, including one or more canisters and comprising: an initial adsorbent volume having an effective incremental adsorption capacity at 25° C. of greater than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane; and at least one subsequent adsorbent volume having an effective incremental adsorption capacity at 25° C. of less than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane, and an effective butane working capacity (BWC) of less than 3 g/dL, wherein the initial adsorbent volume and the at least one subsequent adsorbent volume are located within a single canister, or the initial adsorbent volume and the at least one subsequent adsorbent volume are located in separate canisters that are connected to permit sequential contact by fuel vapor, wherein the canister system has a two-day diurnal breathing loss (DBL) emissions of no more than 20 mg as determined by the 2012 California Bleed Emissions Test Procedure (BETP).
 53. The canister system of claim 52, wherein the two-day DBL is no more than 20 mg at no more than 210 liters of purge applied after a 40 g/hr butane loading step.
 54. The canister system of claim 52 wherein the at least one subsequent adsorbent volume has a g-total BWC of between 2 g and 6 g.
 55. The canister system of claim 52, wherein the two-day DBL is no more than 20 mg at no more than 100 bed volumes (BV) of purge applied after a 40 g/hr butane loading step.
 56. An evaporative emission control canister system, including one or more canisters and comprising: an initial adsorbent volume having an effective incremental adsorption capacity at 25° C. of greater than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane; at least one subsequent adsorbent volume having an effective incremental adsorption capacity at 25° C. of less than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane, and an effective butane working capacity (BWC) of less than 3 g/dL; and a heat input unit for heating one or more adsorbent volumes, wherein the initial adsorbent volume and the at least one subsequent adsorbent volume are located within a single canister, or the initial adsorbent volume and the at least one subsequent adsorbent volume are located in separate canisters that are connected to permit sequential contact by fuel vapor, wherein the canister system has a two-day diurnal breathing loss (DBL) emissions of no more than 20 mg as determined by the 2012 California Bleed Emissions Test Procedure (BETP).
 57. The canister system of claim 56, wherein the two-day DBL is no more than 20 mg at no more than 210 liters of purge applied after a 40 g/hr butane loading step.
 58. The canister system of claim 57 wherein the at least one subsequent adsorbent volume has a g-total BWC of between 2 g and 6 g.
 59. The canister system of claim 56, wherein the two-day DBL is no more than 20 mg at no more than 100 bed volumes (BV) of purge applied after a 40 g/hr butane loading step.
 60. An evaporative emission control canister system, including one or more canisters and comprising: an initial adsorbent volume having an effective incremental adsorption capacity at 25° C. of greater than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane; and at least one subsequent adsorbent volume having an effective incremental adsorption capacity at 25° C. of less than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane, and a g-total BWC of ≦6 grams, wherein the initial adsorbent volume and the at least one subsequent adsorbent volume are located within a single canister, or the initial adsorbent volume and the at least one subsequent adsorbent volume are located in separate canisters that are connected to permit sequential contact by fuel vapor, wherein the two-day DBL is no more than 20 mg at no more than 100 bed volumes (BV) of purge applied after a 40 g/hr butane loading step.
 61. The canister system of claim 60 wherein the at least one subsequent adsorbent volume has a g-total BWC of between 2 g and 6 g.
 62. The canister system of claim 60 wherein the at least one subsequent adsorbent volume has a an effective butane working capacity (BWC) of less than 3 g/dL.
 63. An evaporative emission control canister system, including one or more canisters and comprising: an initial adsorbent volume having an effective incremental adsorption capacity at 25° C. of greater than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane; and at least one subsequent adsorbent volume having an effective incremental adsorption capacity at 25° C. of less than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane, and a g-total BWC of ≦6 grams; and a heat input unit for heating one or more adsorbent volumes, wherein the initial adsorbent volume and the at least one subsequent adsorbent volume are located within a single canister, or the initial adsorbent volume and the at least one subsequent adsorbent volume are located in separate canisters that are connected to permit sequential contact by fuel vapor, wherein the two-day DBL is no more than 20 mg at no more than 100 bed volumes (BV) of purge applied after a 40 g/hr butane loading step.
 64. The canister system of claim 60 wherein the at least one subsequent adsorbent volume has a g-total BWC of between 2 g and 6 g.
 65. The canister system of claim 60 wherein the at least one subsequent adsorbent volume has a an effective butane working capacity (BWC) of less than 3 g/dL. 